EP0567388B1 - Procédé pour la séparation d'un composé organique volatil d'un gaz - Google Patents

Procédé pour la séparation d'un composé organique volatil d'un gaz Download PDF

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Publication number
EP0567388B1
EP0567388B1 EP93401017A EP93401017A EP0567388B1 EP 0567388 B1 EP0567388 B1 EP 0567388B1 EP 93401017 A EP93401017 A EP 93401017A EP 93401017 A EP93401017 A EP 93401017A EP 0567388 B1 EP0567388 B1 EP 0567388B1
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Prior art keywords
absorption
column
liquid
gas
absorption column
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EP93401017A
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German (de)
English (en)
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EP0567388A1 (fr
Inventor
Osamu C/O Showa Shell Sekiyu K.K. Yamase
Yasuyuki c/o SHOSEKI ENGENEERING COMPANY Makita
Kazuyoshi c/o SHOSEKI ENGENEERING COMPANY Jajima
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Showa Shell Sekiyu KK
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Showa Shell Sekiyu KK
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1406—Multiple stage absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1412—Controlling the absorption process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1487—Removing organic compounds

Definitions

  • the present invention relates to a technology by which a volatile organic compound can be recovered effectively from a mixed gas containing the organic compound in the state of gas to avoid the compound from being diffused in atmospheric air.
  • Volatile hydrocarbons are diffused from storage tanks in atmospheric air when atmospheric temperature rises. Also, the volatile hydrocarbons are diffused in atmospheric air when they are flowed into storage tanks or when they are filled in tank lorries from storage tanks. Diffused hydrocarbons are said to form substances causing "photochemical smog". Accordingly, regulations have been carried out in Japan and other countries to control the concentration of the hydrocarbons in an exhaust or flue gas, and severer regulations have lately been issued in several countries, the United States being a leading country.
  • a standard hydrocarbon concentration in the exhaust or flue gases at outlets is established under a prefectural regulation in Nagoya, Japan, which is the severest regulation in the past and by which the hydrocarbon concentration at the outlets is prescribed to be lower than 5% by volume (corresponding to about 80% by volume in terms of the recovery (as referred hereinafter) of hydrocarbon from a gas having a hydrocarbon concentration of 21% by volume at inlets).
  • VOC volatile organic compound
  • the hydrocarbon vapor In the adsorption method, however, there is a danger of firing since a large amount of the heat of adsorption will be generated.
  • the hydrocarbon vapor In the low temperature processing method, the hydrocarbon vapor must be cooled down to a temperature lower than -35°C in order to increase the recovery percentage since the vapor has a very low liquefying temperature and thus this method is economically disadvantageous.
  • Suitable liquids used for the absorption are ones which are insoluble in water, have a strong absorption power to hydrocarbon gas, and having such a low vapor pressure such that the liquids will not be lost when hydrocarbon is separated for recovery.
  • the liquids comprise, as a major component, at least one compound selected from the group consisting of phthalic acid esters, silicic acid esters, phosphoric acid esters, fatty acid esters, alkylbenzene, alkylnaphthalene, and ⁇ -olefins .
  • the liquids may additionally contain less than 75% by weight of a refined mineral oil having a viscosity of 5 to 20 cst at a temperature of 37.8°C, a boiling point of 250 to 450°C, and an average molecular weight of 200 to 350.
  • the hydrocarbon concentration at the outlets can be controlled lower than 5% by volume by using a system composed of an absorption column, desorption column, recovery column, and vacuum pump.
  • the absorption method has a defect that a severer standard regulated under, for example, the EPA in the United States can not be cleared.
  • the volatile organic compound will remain in the desorption column in an amount corresponding to the compound's vapor pressure under a reduced pressure at the stage of regeneration of the absorption liquid in the desorption column, and the remaining compound will obstruct the increase of the recovery percentage of volatile organic compound in the absorption column.
  • the object of the present invention is to provide a novel method for separating or recovering a volatile organic compound from a gas or vapor of gasoline, kerosene, benzene, or alcohol discharged from storage tanks, tank trucks, or tank lorries at a recovery of 90 to 96% by volume.
  • gas as used hereinafter is intended to have the meaning of gas, vapor and mist.
  • the present invention relates to processes for separating a volatile organic compound from a gas containing the organic compound according to claims 1-4.
  • Fig. 1 is a graph showing the relationship between the pressure in a desorption column and a concentration of a volatile organic compound contained in a gas to be introduced into a first absorption column.
  • Fig. 2 is a first flow diagram of a system for conducting the process according to the present invention.
  • Fig. 3 is a second flow diagram of a system for conducting the process according to the present invention.
  • Fig. 4 is a flow diagram of a modified system for conducting the process of the present invention.
  • P is an operating pressure (mmHg) in a first and second desorption column
  • f is a concentration (molar fraction) of a volatile organic compound in a gas to be introduced into the first absorption column at a lower part in the first absorption column.
  • the equation A shows the relationship between the concentration of a volatile organic compound in the feed gas and an operating pressure at the first and second desorption column keeping out of explosion limit of the second desorption column outlet gas by regulating air injection rate to the second desorption column at a recovery of 95% by volume of a volatile organic compound.
  • the equation A' shows the relationship between the concentration of a volatile organic compound in the feed gas and an operating pressure at the first and second desorption column keeping out of explosion limit of the second desorption column outlet gas by regulating air injection rate to the second desorption column at a recovery of 90% by volume of a volatile organic compound.
  • the amount of entrainment of the liquid accompanied with the evaporation of hydrocarbon will increase with increase in the amount of volatile organic compound contained in the rich oil, and 35% by mole (10% by weight) is an upper limit of the amount of the volatile organic compound which is permitted to contain in the rich oil, derived empirically through actual operation and from the view point of safety. When the amount is more than 35% by mole, the entrainment will occur such an extent that operation is impossible.
  • the concentration of the hydrocarbon in the rich oil will decrease with decrease in the concentration of the hydrocarbon in the gas to be fed to the first absorption column, since the amount of hydrocarbon accumulated in the liquid will decrease.
  • the pressure in the first desorption column necessary to secure the amount in the liquid at lower than 35% by mole may become higher with decrease in the concentration of the hydrocarbon in the gas to be fed into the first absorption column.
  • the second desorption column is operated at the same pressure as the first desorption column.
  • the line C shows the relationship between operating pressure P necessary when the air is not bubbled and concentration f of a volatile organic compound in the gas to be fed into the first absorption column at a lower part in the first absorption column at a recovery of the volatile organic compound of 95% by volume.
  • Fig. 2 is a first flow diagram of a system for conducting a first and third embodiments of the present invention.
  • a gas containing the organic compound for example a hydrocarbon gas
  • a liquid for first absorption introduced through a line 13 into the first absorption column at an upper part in the first absorption column to separate a major portion of the organic compound from the gas.
  • the gas thus treated is introduced through a line 14 into a second absorption column at a lower part in the second absorption column 2.
  • the liquid which absorbed the volatile organic compound in the first absorption column 1 is introduced through a line 12 into a first desorption column 3 at an upper part in the first desorption column 3.
  • Operating conditions for the first desorption column are determined so that the conditions of the present invention are satisfied.
  • the volatile organic compound is separated from the absorption liquid.
  • Absorption liquid from which the volatile organic compound was separated is recycled through a line 13 back to the first absorption column 1 as the liquid for first absorption.
  • the gas containing the organic compound separated in the second desorption column is fed through lines 17 and 19 to a column 5 for recovering the volatile organic compound.
  • a liquid for recovering the volatile organic compound is supplied through a line 20 to an upper part in the recovery column 5.
  • the volatile organic compound is recovered from a line 21, and a treated gas is recycled backed to the first absorption column 1.
  • a liquid (second absorption liquid) which absorbed a remaining organic compound in the second absorption column is introduced through a line 15 into a second desorption column 4 at an upper part in the second desorption column.
  • the second absorption liquid from which the volatile organic compound was separated is recycled through a line 16 back to the second absorption column 2.
  • the gaseous organic compound separated in the second desorption column is fed through lines 17 and 19 to the column 5 for recovering the volatile organic compound.
  • Fig. 3 is a second flow diagram of a system for conducting a second and fourth embodiments of the present invention.
  • the diagram is the same as that of Fig. 2 except that an air introducing pipe 23 for air bubbling is connected to a lower part in the second desorption column 4.
  • Fig. 4 is a flow diagram of a modified system of the process of the present invention in which a third desorption column 6 is provided below the second desorption column 4 shown in Fig. 3, and air bubbling is conducted in a third desorption column 6.
  • the relationship between the pressure (regeneration pressure) in each of the desorption columns and the concentration of a so-called inert component other than the hydrocarbon is not affected even if a gas flow rate was varied.
  • air introducing rate and total flow rate in a vacuum pump are varied in proportion to gas flow rate.
  • Example 1 (Tables 4 to 5), air was bubbled in the second desorption column at a gas flow rate of 1000 Nm 3 /hr at the inlet in the first absorption column, and in Example 3 (Tables 8 to 9), air was not bubbled but the inlet gas flow rate was the same as in Example 1.
  • the recovery of the hydrocarbon was aimed at 90% by volume in both Examples.
  • Example 1 The pressure in the first and second desorption columns in Example 1 (Tables 4 to 5) was higher than that in Example 3 (Tables 8 to 9) since air was bubbled in Example 1.
  • the necessary gas flow rate of vacuum pump was 98 m 3 /min at maximum in Example 1 (Tables 4 to 5) while the necessary gas flow rate was 110 m 3 /min in Example 3 (Tables 8 to 9) at maximum. This indicates that the necessary gas flow rate of a vacuum pump was higher by 12 m 3 /min in Example 3 wherein air was not bubbled.
  • Example 2 (Tables 6 to 7), air was bubbled in the second desorption column at a gas flow rate of 1000 Nm 3 /hr at the inlet in the first absorption column, and in Example 4 (Tables 10 to 11), air was not bubbled but the inlet gas flow rate was the same as in Example 2.
  • the recovery of the hydrocarbon was aimed at 95% by volume in both Examples.
  • Example 2 The pressure in the first and second desorption columns in Example 2 (Tables 6 to 7) was higher than that in Example 4 (Tables 10 to 11) since air was bubbled in Example 2.
  • the necessary gas flow rate of vacuum pump was 160 m 3 /min at maximum in Example 2 (Tables 6 to 7) while the necessary gas flow rate was 200 m 3 /min in Example 4 (Tables 10 to 11) at maximum. This indicates that the necessary gas flow rate of a vacuum pump was higher by 40 m 3 /min in Example 4 wherein air was not bubbled.
  • Example 2 As in the cases in Examples 2 and 4, calculation was performed for the number of necessary vacuum pumps having a rated capacity of 50 m 3 /min (at a suction pressure of 25 mmHg) from the data shown in Tables 6 to 7 and 10 to 11 to obtain the results that 2.5 to 3.8 vacuum pumps are necessary to be used in Example 2 (Tables 6 to 7) while 3.1 to 7.1 vacuum pumps are necessary in Example 4 (Tables 10 to 11) as shown in detail in Table 2. Table 2 Number of necessary vacuum pumps (rated capacity 50 m 3 /min, gas recovery 95% by volume) Hydrocarbon concentration in feeding gas (%) 10.6 12.7 16.0 19.9 24.6 30 36.5 40.2 Example 4 Air was not bubbled. 7.1 5.8 5.1 4.5 4.4 3.6 3.3 3.1 Example 2 Air was bubbled. 3.8 3.5 3.4 3.3 2.8 2.7 2.5 2.5
  • a rational or effective plant can be designed by obtaining best operating conditions for a minimum plant cost through a simulation at a required gas recovery to be aimed.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (4)

  1. Un procédé permettant de recueillir plus de 90 % en volume de composés organiques volatils à partir d
    Figure imgb0031
    Figure imgb0031
    un gaz les contenant et qui consiste à
    introduire le gaz de départ par l
    Figure imgb0031
    extrémité inférieure d
    Figure imgb0031
    une première colonne d
    Figure imgb0031
    absorption,
    introduire un liquide d
    Figure imgb0031
    absorption dans une partie supérieure de la première colonne d
    Figure imgb0031
    absorption pour que le liquide vienne en contact à contre-courant avec le gaz de telle sorte qu
    Figure imgb0031
    il absorbe une fraction prépondérante des composés organiques présents dans le gaz,
    introduire le gaz qui sort de la première colonne d
    Figure imgb0031
    absorption et qui contient les composés organiques restants dans une partie inférieure d
    Figure imgb0031
    une deuxième colonne d
    Figure imgb0031
    absorption,
    introduire un autre liquide d
    Figure imgb0031
    absorption dans une partie supérieure de la seconde colonne d
    Figure imgb0031
    absorption de telle sorte que le liquide vienne en contact à contre-courant avec le gaz provenant de la première colonne d
    Figure imgb0031
    absorption,
    envoyer le premier liquide d
    Figure imgb0031
    absorption qui sort d'une partie inférieure de la première colonne d
    Figure imgb0031
    absorption à une partie supérieure d
    Figure imgb0031
    une première colonne de désorption,
    recycler le liquide qui sort d'une partie inférieure de la première colonne de désorption à nouveau dans la première colonne d
    Figure imgb0031
    absorption, en tant que liquide d
    Figure imgb0031
    absorption,
    envoyer le liquide d
    Figure imgb0031
    absorption qui sort de la partie inférieure de la deuxième colonne d
    Figure imgb0031
    absorption à une partie supérieure d
    Figure imgb0031
    une deuxième colonne de désorption,
    recycler le liquide qui sort de la partie inférieure de la deuxième colonne de désorption à nouveau à la deuxième colonne d
    Figure imgb0031
    absorption en tant que liquide d
    Figure imgb0031
    absorption, et
    recueillir les composés organiques volatils restants,
    caractérisé en ce qu'il consiste à maintenir les pressions de fonctionnement dans la première et la deuxième colonne de désorption au même niveau P (mm de Hg), et à régler la pression P (mm de Hg) et la concentration f (fraction molaire) des composés organiques volatils qui sont présents dans le gaz à charger dans la première colonne d
    Figure imgb0031
    absorption, de sorte qu'à la fois les trois formules soient satisfaites: (C') P ≦ 8,31 + 51 f + 200 f 2 (B) P ≦ - 70 f + 83 (D). 0,10 ≦ f ≦ 0,40
    Figure imgb0056
  2. Un procédé permettant de recueillir plus de 90 % en volume de composés organiques volatils à partir d
    Figure imgb0031
    un gaz les contenant et qui consiste à
    introduire le gaz de départ par l
    Figure imgb0031
    extrémité inférieure d
    Figure imgb0031
    une première colonne d
    Figure imgb0031
    absorption,
    introduire un liquide d
    Figure imgb0031
    absorption dans une partie supérieure de la première colonne d
    Figure imgb0031
    absorption pour que le liquide vienne en contact à contrecourant avec le gaz de telle sorte qu
    Figure imgb0031
    il absorbe une fraction prépondérante des composés organiques présents dans le gaz,
    introduire le gaz qui sort de la première colonne d
    Figure imgb0031
    absorption et qui contient les composés organiques restants dans une partie inférieure d
    Figure imgb0031
    une deuxième colonne d
    Figure imgb0031
    absorption,
    introduire un autre liquide d
    Figure imgb0031
    absorption dans une partie supérieure de la seconde colonne d
    Figure imgb0031
    absorption de telle sorte que le liquide vienne en contact à contre-courant avec le gaz provenant de la première colonne d
    Figure imgb0031
    absorption,
    envoyer le premier liquide d
    Figure imgb0031
    absorption qui sort d'une partie inférieure de la première colonne d
    Figure imgb0031
    absorption à une partie supérieure d
    Figure imgb0031
    une première colonne de désorption,
    recycler le liquide qui sort d'une partie inférieure de la première colonne de désorption à nouveau dans la première colonne d
    Figure imgb0031
    absorption, en tant que liquide d
    Figure imgb0031
    absorption,
    envoyer le liquide d
    Figure imgb0031
    absorption qui sort de la partie inférieure de la deuxième colonne d
    Figure imgb0031
    absorption à une partie supérieure d
    Figure imgb0031
    une deuxième colonne de désorption,
    recycler le liquide qui sort de la partie inférieure de la deuxième colonne de désorption à nouveau à la deuxième colonne d
    Figure imgb0031
    absorption en tant que liquide d
    Figure imgb0031
    absorption, et
    recueillir les composés organiques volatils restants
    caractérisé en ce qu'il consiste à maintenir les pressions de fonctionnement de la première et de la deuxième colonne de désorption au même niveau P (mm de Hg), à introduire de l
    Figure imgb0031
    air à la partie inférieure de la deuxième colonne de désorption et à régler la pression P (mm de Hg) et la concentration f (fraction molaire) des composés organiques volatils qui sont présents dans le gaz à charger dans la première colonne d
    Figure imgb0031
    absorption de sorte qu'à la fois les trois équations suivantes soient vérifiées: (A') P ≦ 380 f / (1 - 0,90 f) (B) P ≦ - 70 f + 83 (D). 0,10 ≦ f ≦ 0,40
    Figure imgb0082
  3. Un procédé permettant de recueillir plus de 95 % en volume de composés organiques volatils à partir d
    Figure imgb0031
    un gaz les contenant et qui consiste à
    introduire le gaz de départ par l
    Figure imgb0031
    extrémité inférieure d
    Figure imgb0031
    une première colonne d
    Figure imgb0031
    absorption,
    introduire un liquide d
    Figure imgb0031
    absorption dans une partie supérieure de la première colonne d
    Figure imgb0031
    absorption pour que le liquide vienne en contact à contrecourant avec le gaz de telle sorte qu
    Figure imgb0031
    il absorbe une fraction prépondérante des composés organiques présents dans le gaz,
    introduire le gaz qui sort de la première colonne d
    Figure imgb0031
    absorption et qui contient les composés organiques restants dans une partie inférieure d
    Figure imgb0031
    une deuxième colonne d
    Figure imgb0031
    absorption,
    introduire un autre liquide d
    Figure imgb0031
    absorption dans une partie supérieure de la seconde colonne d
    Figure imgb0031
    absorption de telle sorte que le liquide vienne en contact à contre-courant avec le gaz provenant de la première colonne d
    Figure imgb0031
    absorption,
    envoyer le premier liquide d
    Figure imgb0031
    absorption qui sort d'une partie inférieure de la première colonne d
    Figure imgb0031
    absorption à une partie supérieure d
    Figure imgb0031
    une première colonne de désorption,
    recycler le liquide qui sort d'une partie inférieure de la première colonne de désorption à nouveau dans la première colonne d
    Figure imgb0031
    absorption, en tant que liquide d
    Figure imgb0031
    absorption,
    envoyer le liquide d
    Figure imgb0031
    absorption qui sort de la partie inférieure de la deuxième colonne d
    Figure imgb0031
    absorption à une partie supérieure d
    Figure imgb0031
    une deuxième colonne de désorption,
    recycler le liquide qui sort de la partie inférieure de la deuxième colonne de désorption à nouveau à la deuxième colonne d
    Figure imgb0031
    absorption en tant que liquide d
    Figure imgb0031
    absorption, et
    recueillir les composés organiques volatils restants,
    caractérisé en ce qu'il consiste à maintenir les pressions de fonctionnement, P (mm de Hg), dans la première et la deuxième colonne de désorption, au même niveau, et à régler la pression P et la fraction molaire, f, des composés organiques volatils présents dans le gaz à charger dans la première colonne d
    Figure imgb0031
    absorption, de sorte que les deux équations suivantes soient vérifiées: (C) P ≦ 3,86 + 45 f + 75,1 f 2 (D). 0,10 ≦ f ≦ 0,40
    Figure imgb0107
  4. Un procédé permettant de récupérer un volume supérieur à 95 % de composés organiques volatils à partir d
    Figure imgb0031
    un gaz les contenant et qui consiste à
    introduire le gaz de départ par l'extrémité inférieure d
    Figure imgb0031
    une première colonne d
    Figure imgb0031
    absorption,
    introduire le liquide d
    Figure imgb0031
    absorption par le haut de la première colonne d'absorption pour que le liquide vienne en contact à contre-courant avec le gaz de telle sorte à absorber une fraction importante des composés organiques présents dans le gaz,
    introduire le gaz sortant de la première colonne d'absorption, et qui contient encore des composés organiques, par l'extrémité inférieure d
    Figure imgb0031
    une deuxième colonne d
    Figure imgb0031
    absorption,
    introduire un autre liquide d
    Figure imgb0031
    absorption par le haut de la seconde colonne d
    Figure imgb0031
    absorption de telle sorte que le liquide vienne en contact à contre-courant avec le gaz provenant de la première colonne d'absorption,
    introduire le premier liquide d
    Figure imgb0031
    absorption qui sort par le bas de la première colonne d
    Figure imgb0031
    absorption en haut d
    Figure imgb0031
    une première colonne de désorption,
    recycler le liquide qui sort par le bas de la première colonne de désorption en l
    Figure imgb0031
    introduisant à nouveau dans la première colonne d
    Figure imgb0031
    absorption, en tant que liquide d
    Figure imgb0031
    absorption,
    introduire le deuxième liquide d'absorption, qui sort à l'extrémité inférieure de la deuxième colonne d'absorption, en haut d'une deuxième colonne de désorption,
    recycler le liquide qui sort par l'extrémité inférieure de la deuxième colonne de désorption en l'introduisant à nouveau dans la deuxième colonne d'adsorption en tant que liquide d'absorption, et
    récupérer les composés organiques volatils restants
    caractérisé en ce qu'il consiste à maintenir les pressions de fonctionnement, P (mm de Hg), de la première et de la deuxième colonne de désorption au même niveau, à introduire de l
    Figure imgb0031
    air par le bas de la deuxième colonne de désorption et à régler la pression P et la fraction molaire, f, des composés organiques volatils présents dans le gaz à charger dans la première colonne d
    Figure imgb0031
    absorption de telle sorte que les trois équations suivantes soient vérifiées: (A) P ≦ 190 f / (1 - 0,95 f) (B) P ≦ - 70 f + 83 (D). 0,10 ≦ f ≦ 0,40
    Figure imgb0124
EP93401017A 1992-04-21 1993-04-20 Procédé pour la séparation d'un composé organique volatil d'un gaz Expired - Lifetime EP0567388B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP4128063A JPH05293332A (ja) 1992-04-21 1992-04-21 揮発性有機化合物含有ガスの除去方法
JP128063/92 1992-04-21

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EP0567388A1 EP0567388A1 (fr) 1993-10-27
EP0567388B1 true EP0567388B1 (fr) 1996-09-18

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US (1) US5330563A (fr)
EP (1) EP0567388B1 (fr)
JP (1) JPH05293332A (fr)
DE (1) DE69304773T2 (fr)

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DE4338003A1 (de) * 1993-11-07 1995-05-11 Dynamit Nobel Ag Verfahren zur Abtrennung von organischen Komponenten aus Abluft
GB9413714D0 (en) * 1994-07-07 1994-08-24 Turbotak Technologies Inc Regenerative process for removal and recovery of volatile organic compounds (VOCs) from effluent gases
US6726750B2 (en) 2000-06-05 2004-04-27 Ch2M Hill, Inc. Apparatus and method for efficient recovery of volatile organic compounds
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US5330563A (en) 1994-07-19
DE69304773D1 (de) 1996-10-24
DE69304773T2 (de) 1997-04-30
EP0567388A1 (fr) 1993-10-27
JPH05293332A (ja) 1993-11-09

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